EP0845452A1 - Verfahren III zur Herstellung von Essigsäure - Google Patents

Verfahren III zur Herstellung von Essigsäure Download PDF

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Publication number
EP0845452A1
EP0845452A1 EP97120083A EP97120083A EP0845452A1 EP 0845452 A1 EP0845452 A1 EP 0845452A1 EP 97120083 A EP97120083 A EP 97120083A EP 97120083 A EP97120083 A EP 97120083A EP 0845452 A1 EP0845452 A1 EP 0845452A1
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Prior art keywords
acetic acid
carbon monoxide
stream
methanol
liquid
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EP97120083A
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English (en)
French (fr)
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EP0845452B2 (de
EP0845452B1 (de
Inventor
Finn Joensen
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Topsoe AS
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Haldor Topsoe AS
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Application filed by Haldor Topsoe AS filed Critical Haldor Topsoe AS
Priority to DE69714554T priority Critical patent/DE69714554T3/de
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
    • C07C41/01—Preparation of ethers
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
    • C07C51/12—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on an oxygen-containing group in organic compounds, e.g. alcohols
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to preparation of acetic acid from a synthesis gas of hydrogen and carbon oxides. More particular, the invention comprises catalytic steps of converting hydrogen and carbon monoxide in the gas to a process stream containing methanol or methanol/dimethyl ether (DME) and carbonylating methanol or methanol/DME formed in the process stream into acetic acid.
  • DME dimethyl ether
  • the conventional process for the manufacture of acetic acid presently widely used in the industry includes catalytic carbonylation of methanol as disclosed by e.g. US Patent No. 3,769,329 and EP Patent No. 250,189.
  • Catalysts usually employed in the carbonylation reaction comprise a rhodium compound promoted with methyl iodide.
  • the conventional acetic acid process requires supply of methanol reactant from external sources.
  • a possible route to eliminate the need for external supply of methanol may be to integrate synthesis of methanol into the acetic acid process by producing methanol and carbon monoxide in parallel.
  • This approach is, in particular, convenient when both reactants are prepared from synthesis gas obtained at high efficiency through steam reforming of natural gas.
  • Simultaneous preparation of methanol and DME from hydrogen and carbon oxides containing synthesis gas is catalyzed by a number of catalysts such as the known methanol catalyst including mixed oxides of Cu/Zn/Cr or Cu/Zn/Al and methanol dehydration catalysts such as alumina, silica-alumina, zeolitic materials, silica alumino phosphates and heteropoly acids of Mo and W being applied as physical mixture or prepared by impregnation on carrier materials, co-pelletization or co-precipitation.
  • methanol catalyst including mixed oxides of Cu/Zn/Cr or Cu/Zn/Al
  • methanol dehydration catalysts such as alumina, silica-alumina, zeolitic materials, silica alumino phosphates and heteropoly acids of Mo and W being applied as physical mixture or prepared by impregnation on carrier materials, co-pelletization or co-precipitation.
  • Acetic acid preparation from a hydrogen and carbon monoxide containing synthesis gas including synthesis of methanol and DME at a high hydrogen/carbon monoxide ratio in the synthesis gas in a first catalytic reaction stage and subsequent carbonylation of the effluent from the first reaction stage to acetic acid product with added carbon monoxide are described in Danish Patent Application No. 96/0407.
  • this invention is a process for the preparation of acetic acid product through: conversion of a hydrogen and carbon monoxide containing synthesis gas to obtain a liquid process stream comprising methanol and, subsequently, in carbonylation of the process stream with carbon monoxide to a product stream being rich in the acetic acid product in presence of catalytic effective amounts of a metal compound selected from Group VIII of the Periodic Table promoted with a halide compound, the improvement comprising further steps of:
  • the process stream to be carbonylated contains a mixture of methanol and dimethyl ether.
  • Those catalysts include the aforementioned catalysts and, in particular, catalysts having a composition of about 60 atom% Cu, 25 atom% Zn and 15 atom% Al being highly active in the methanol forming reaction (2) and alumina or alumina silicates for the DME reaction (3).
  • the catalysts in the first process step may be arranged in a fixed bed of an intimately admixture or as a layered bed with alternating methanol synthesis and methanol dehydration catalyst particles. Physical mixtures of the catalyst result, however, in lower selectivity and it is often preferred to employ a fixed bed of a catalyst composition with combined methanol, and methanol dehydration activity.
  • Such catalyst composition may be prepared by impregnation, copelletization or coprecipitation of the catalytic active materials in accordance with the known methods in the manufacture of catalysts.
  • the process of this invention may be operated advantageously with a high hydrogen/carbon monoxide ratio in the feed gas to the methanol/DME reaction.
  • the hydrogen/carbon monoxide ratio required in the feed gas is typically between 2:1 and 3:1, as supplied by unadjusted synthesis gas from conventional steam reforming of a hydrocarbon feedstock.
  • substantially all amounts of carbon monoxide in the feed gas are converted to DME and methanol and formation of inert carbon dioxide by-product are considerably reduced. Conversion levels similar to those of the conventional methanol synthesis are achieved at a synthesis pressure of 25-50 bar, which correspond to the required pressure in the subsequent acetic acid reaction step.
  • Produced methanol, DME and water are recovered in a liquid process phase from the effluent of the above reaction step by cooling the effluent and recycling of the gaseous phase containing unconverted feed gas and carbon dioxide. A minor part of the gaseous phase is purged to avoid build-up of inerts, such as nitrogen, argon and methane, in the synthesis loop. Due to the relatively high vapour pressure of DME, the purge gas contains further a part of produced DME. Therefore, it is preferred to subject the purge gas from the above effluent to a purge wash with a suitable liquid washing agent, preferably methanol or acetic acid. DME recovered from the purge gas is then combined with the liquid process phase.
  • a suitable liquid washing agent preferably methanol or acetic acid
  • catalytic carbonylation of DME and methanol to acetic acid are carried out with carbon monoxide being supplied to the reaction as a separate stream.
  • Carbon monoxide is introduced into the carbonylation step in an amount corresponding at least to the stoichiometric amount in the carbonylation reaction: CH 3 OH + CO ⁇ CH 3 COOH CH 3 OCH 3 + 2CO + H 2 O ⁇ 2CH 3 COOH
  • the monoxide will be added in an amount resulting in a mole ratio of carbon monoxide and methanol plus DME, i.e. CO/(CH 3 OH + 2CH 3 OCH 3 ), in the carbonylation reaction in the range of between 1 to 1.5.
  • Catalysts usually employed are based on a combination of Group VIII transition metal compounds and a halogen compound promoter.
  • a number of secondary promoters have been disclosed in the art, comprising metal salts and organic compounds.
  • Preferred catalysts for use in the invention include compounds of group VIII metals of the Periodic System promoted with iodine or bromine compounds, e.g. methyl iodide.
  • the carbonylation reactions may be carried out within a wide range of temperatures from about 100°C to 400°C, though temperatures between 150°C and 250°C are sufficient to obtain reasonable reaction conditions.
  • the reaction is performed in liquid phase at elevated pressure by establishing a partial pressure of the carbon monoxide in the gas phase over the liquid reaction phase in the reactor being sufficiently high to provide sufficient concentration of dissolved carbon monoxide in the liquid phase for the carbonylation reactions proceeding in this phase.
  • the pressure will be in the range of 25-50 bar depending on the reaction temperature and catalyst concentration.
  • Carbon monoxide is usually introduced continuously at the bottom of the reactor and bubbled through the liquid process phase in a predetermined amount to reach the desired yield of acetic acid product in the carbonylation reactions as mentioned above.
  • Carbon monoxide may be supplied from a substream of the carbon monoxide containing synthesis gas by conventional separation methods, such as cryogenic separation or separation of the monoxide in a membrane unit, wherein hydrogen in the gas with high selectivity permeates through a hollow fibre membrane, and carbon monoxide is recovered in the residue stream of the membrane unit.
  • conventional separation methods such as cryogenic separation or separation of the monoxide in a membrane unit, wherein hydrogen in the gas with high selectivity permeates through a hollow fibre membrane, and carbon monoxide is recovered in the residue stream of the membrane unit.
  • reaction step part of carbon monoxide is converted into carbon dioxide through the water gas shift reaction: CO + H 2 O ⁇ CO 2 + H 2
  • the carbon monoxide reactant gas usually contains small amounts of inerts such as methane, nitrogen and argon.
  • inerts such as methane, nitrogen and argon.
  • the overhead gas phase must be vented by passing an excess amount of carbon monoxide through the reaction solution.
  • vent gas being rich in carbon monoxide
  • concentration of hydrogen, carbon dioxide and inerts in the gas phase are maintained at an acceptable low level.
  • the vent gas contains methyl iodide, water and acetic acid vapours.
  • the gas stream is cooled whereby part of the condensible fraction is recovered and recycled to the reactor.
  • the gaseous phase still contains considerable amounts of methyl iodide.
  • the gas is passed to a methyl iodide absorber where methyl iodide is absorbed in a liquid absorption medium, preferably acetic acid or aqueous acetic acid and subsequently stripped off in a methyl iodide stripper column and returned to the carbonylation step.
  • the purge gas from the absorber unit consists of carbon monoxide, hydrogen, carbon dioxide and inerts together with traces of methyl iodide.
  • the gas further contains minor amounts of the acetic acid absorption agent. Due to the content of hydrogen, carbon dioxide and inerts, the purge gas cannot be recycled to the carbonylation step.
  • vent gas is advantageously utilized in the synthesis gas conversion reactions allowing for the efficient conversion of carbon monoxide, hydrogen and carbon dioxide into methanol or methanol/dimethyl ether.
  • vent gas to be recycled inevitably contains small amounts of the acetic acid washing agent as well as traces of methyl iodide. Both substances may act as inhibitors or even poison to the catalysts applied in the synthesis gas conversion step. It is, therefore, necessary that acetic acid and methyl iodide traces are efficiently removed before introducing the vent gas stream into the conversion step.
  • vent gas is introduced into the liquid product phase obtained in the synthesis gas conversion step consisting of methanol, dimethyl ether and water and using the liquid phase as a second washing agent for the removal of acetic acid and traces of methyl iodide.
  • the vent gas is introduced countercurrently to the liquid product flow in liquid product separator.
  • the bottom of separator is, therefore, preferably equipped with trays or packing material to improve the absorption process.
  • vent gas is introduced directly to the liquid product phase obtained in the synthesis gas conversion step without being passed through a methyl iodide absorber.
  • the reactor effluent stream 3 is cooled to produce a liquid phase containing methanol, dimethyl ether and water and a gaseous phase containing hydrogen, carbon monoxide and carbon dioxide and inerts such as methane.
  • the cooled reactor effluent stream is passed to separator 102 from which is withdrawn 9950 kg/h of a liquid process stream 5 containing liquid products of stream 3 and a gaseous stream 4 containing unconverted synthesis gas and inerts. Part of the gaseous stream 4 is purged to avoid build-up of inerts in the synthesis loop and the remainder is recycled as stream 2.
  • Stream 5 is passed to acetic acid reactor 104 in which methanol, dimethyl ether and water are reacted in a second catalytic step with 8760 Nm 3 /h of 93 mole% carbon monoxide, the remainder being hydrogen and methane, added as stream 8 to form acetic acid at a pressure of 35 bar and 185°C by employing a catalyst system comprising a rhodium catalyst and a methyl iodide promoter.
  • part of the carbon monoxide reacts with water to produce carbon dioxide and hydrogen by the water gas shift reaction.
  • a stream 9 of 300 kg/h of water is added to reactor 104 in order to maintain a finite water concentration.
  • the gaseous stream 7 is passed through reflux condenser 105 to recover part of condensibles comprising acetic acid, water and methyl iodide which are recycled to the reactor 104 and the resulting gaseous stream 10 is passed to absorber 106, in which essentially all methyl iodide is recovered by absorption in liquid acetic acid.
  • Example 1 88.4% of the total carbon monoxide contained in the feed streams 1 plus 9 is converted into acetic acid.
  • 27523 Nm 3 /h of a synthesis gas stream 1 are converted in the way described in Example 1 to obtain a reactor effluent stream 3 containing methanol, dimethyl ether and water.
  • the reactor effluent stream 3 is cooled to produce a liquid phase containing methanol, dimethyl ether and water and a gaseous phase containing hydrogen, carbon monoxide and carbon dioxide and inerts such as methane.
  • the cooled reactor effluent stream is passed to absorber 102 and contacted countercurrently with 1520 Nm 3 /h of an acetic acid reactor vent gas stream 12 containing as the main components carbon monoxide, hydrogen and methane and minor amounts of acetic acid and traces of methyl iodide.
  • From the absorber 102 is withdrawn 9960 kg/h of a liquid process stream 5 containing liquid products of stream 3 and acetic acid and traces of methyl iodide contained in stream 12 and a gaseous stream 4 containing unconverted synthesis gas and inerts of the first catalytic step and carbon monoxide, hydrogen, carbon dioxide and inerts of stream 12. Part of the combined gaseous stream 4 is purged to avoid build-up of inerts in the synthesis loop and the remainder is recycled as stream 2.
  • Stream 5 is passed to acetic acid reactor 104 in which methanol, dimethyl ether and water are reacted in a second catalytic step with 8760 Nm 3 /h of 93 mole% carbon monoxide, the remainder being hydrogen and methane, added as stream 8 to form acetic acid as described in Example 1.
  • a stream 9 of 345 kg/h of water is added to reactor 104 in order to maintain a finite water concentration.
  • the gaseous stream 7 is passed through reflux condenser 105 to recover part of condensibles comprising methyl iodide and acetic acid, which are recycled to the reactor 104 and the resulting gaseous stream 10 is passed to absorber 106, in which essentially all methyl iodide is recovered by absorption in liquid acetic acid. From absorber 106, the gaseous stream 12 is passed to the aforementioned absorber 102 for recovery of residual amounts of acetic acid originating from the wash and remaining traces of methyl iodide.
  • acetic acid is produced in a process similar to that of Example 2 except that the gas stream 10 is passed directly to the absorber 102 for recovery of methyl iodide and acetic acid.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
EP97120083A 1996-11-29 1997-11-17 Verfahren III zur Herstellung von Essigsäure Expired - Lifetime EP0845452B2 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
DE69714554T DE69714554T3 (de) 1996-11-29 1997-11-17 Verfahren III zur Herstellung von Essigsäure

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DK199601361A DK136196A (da) 1996-11-29 1996-11-29 Fremgangsmåde til fremstilling af eddikesyre
DK136196 1996-11-29

Publications (3)

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EP0845452A1 true EP0845452A1 (de) 1998-06-03
EP0845452B1 EP0845452B1 (de) 2002-08-07
EP0845452B2 EP0845452B2 (de) 2011-09-14

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EP97120083A Expired - Lifetime EP0845452B2 (de) 1996-11-29 1997-11-17 Verfahren III zur Herstellung von Essigsäure

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US (1) US5840969A (de)
EP (1) EP0845452B2 (de)
JP (1) JP3983868B2 (de)
CN (1) CN1160300C (de)
AT (1) ATE221868T1 (de)
DE (1) DE69714554T3 (de)
DK (1) DK136196A (de)
RU (1) RU2196128C2 (de)
UA (1) UA53620C2 (de)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001032594A1 (en) * 1999-11-01 2001-05-10 Acetex (Cyprus) Limited Methanol plant retrofit for manufacture of acetic acid
US6353133B1 (en) 1999-11-01 2002-03-05 Acetex (Cyprus) Limited Methanol plant retrofit
US6531630B2 (en) 2000-12-29 2003-03-11 Kenneth Ebenes Vidalin Bimodal acetic acid manufacture
US6781014B1 (en) 1999-11-01 2004-08-24 Acetex (Cyprus) Limited Methanol plant retrofit for manufacture of acetic acid
WO2014143840A3 (en) * 2013-03-15 2014-12-04 Celanese International Corporation Process for separating product gas using carbonylation processes

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6596781B1 (en) 2002-05-02 2003-07-22 Chevron U.S.A. Inc. Integrated process for preparing Fischer-Tropsch products and acetic acid from synthesis gas
CA2496839A1 (en) 2004-07-19 2006-01-19 Woodland Chemical Systems Inc. Process for producing ethanol from synthesis gas rich in carbon monoxide
KR20080108605A (ko) 2006-04-05 2008-12-15 우드랜드 바이오퓨엘스 인크. 합성 가스에 의해 바이오매스를 에탄올로 전환시키는 시스템 및 방법
EP2072489A1 (de) * 2007-12-17 2009-06-24 BP p.l.c. Verfahren zur Umwandlung von Kohlenwasserstoffen in Ethanol
US7608744B1 (en) * 2008-07-31 2009-10-27 Celanese International Corporation Ethanol production from acetic acid utilizing a cobalt catalyst
CN101439256B (zh) * 2008-11-14 2011-01-12 江苏索普（集团）有限公司 膜法回收羰基化生产乙酸高压尾气中co的方法及其装置
US8394988B2 (en) 2010-09-28 2013-03-12 Celanese International Corporation Production of acetic acid with high conversion rate
US8877963B2 (en) 2010-09-28 2014-11-04 Celanese International Corporation Production of acetic acid with high conversion rate
WO2012064689A1 (en) * 2010-11-12 2012-05-18 Eastman Chemical Company Processing gaseous streams resulting from carbonylation process
BR112013016630B1 (pt) 2010-12-30 2022-03-03 Celanese International Corporation Composição de resina de troca iônica, leito de proteção e processo para purificar uma composição de ácido acético bruto
US9663437B2 (en) 2011-09-13 2017-05-30 Celanese International Corporation Production of acetic acid with high conversion rate
US9193657B2 (en) * 2012-08-17 2015-11-24 Celanese International Corporation Catalyst stability in carbonylation processes
RU2734824C2 (ru) * 2015-12-18 2020-10-23 Бп Кемикэлз Лимитед Способ карбонилирования с использованием предварительно обработанного цеолитного катализатора
WO2018004994A1 (en) 2016-07-01 2018-01-04 Res Usa, Llc Fluidized bed membrane reactor
US9981896B2 (en) 2016-07-01 2018-05-29 Res Usa, Llc Conversion of methane to dimethyl ether
WO2018004993A1 (en) 2016-07-01 2018-01-04 Res Usa, Llc Reduction of greenhouse gas emission
CN109574839B (zh) * 2017-09-29 2021-08-31 中国科学院大连化学物理研究所 一种合成气直接生产乙酸甲酯和/或乙酸的方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB906008A (en) * 1960-01-23 1962-09-19 Basf Ag Process for the prodution of acetic acid or mixtures of acetic acid and methyl acetate
FR2058060A5 (de) * 1969-08-14 1971-05-21 Ajinomoto Kk
US4110359A (en) * 1976-12-10 1978-08-29 Texaco Development Corporation Production of cleaned and purified synthesis gas and carbon monoxide
US5189203A (en) * 1987-06-30 1993-02-23 Haldor Topsoe A/S Process for preparing acetic acid, methyl acetate, acetic anhydride or mixtures thereof
EP0801050A1 (de) * 1996-04-10 1997-10-15 Haldor Topsoe A/S Verfahren zur Herstellung von Essigsäure

Family Cites Families (5)

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Publication number Priority date Publication date Assignee Title
US3769329A (en) * 1970-03-12 1973-10-30 Monsanto Co Production of carboxylic acids and esters
US4255591A (en) * 1978-11-20 1981-03-10 Monsanto Company Carbonylation process
CA1299195C (en) * 1986-06-16 1992-04-21 G. Paull Torrence Addition of hydrogen to carbon monoxide feed gas in producing acetic acid by carbonylation of methanol
AU639630B2 (en) * 1991-01-28 1993-07-29 Celanese International Corporation Removal of carbonyl impurities from carbonylation process stream
DE19519197A1 (de) * 1995-05-24 1996-11-28 Linde Ag Verfahren zum Rückgewinnen von Kohlenmonoxid aus einem wenigstens Kohlenmonoxid, Stickstoff und Wasserstoff enthaltenden Purgegas der Essigsäuresynthese

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB906008A (en) * 1960-01-23 1962-09-19 Basf Ag Process for the prodution of acetic acid or mixtures of acetic acid and methyl acetate
FR2058060A5 (de) * 1969-08-14 1971-05-21 Ajinomoto Kk
US4110359A (en) * 1976-12-10 1978-08-29 Texaco Development Corporation Production of cleaned and purified synthesis gas and carbon monoxide
US5189203A (en) * 1987-06-30 1993-02-23 Haldor Topsoe A/S Process for preparing acetic acid, methyl acetate, acetic anhydride or mixtures thereof
EP0801050A1 (de) * 1996-04-10 1997-10-15 Haldor Topsoe A/S Verfahren zur Herstellung von Essigsäure

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001032594A1 (en) * 1999-11-01 2001-05-10 Acetex (Cyprus) Limited Methanol plant retrofit for manufacture of acetic acid
US6353133B1 (en) 1999-11-01 2002-03-05 Acetex (Cyprus) Limited Methanol plant retrofit
US6781014B1 (en) 1999-11-01 2004-08-24 Acetex (Cyprus) Limited Methanol plant retrofit for manufacture of acetic acid
AU781369B2 (en) * 1999-11-01 2005-05-19 Acetex (Cyprus) Limited Methanol plant retrofit for manufacture of acetic acid
EP1683780A1 (de) * 1999-11-01 2006-07-26 Acetex (Cyprus) Limited Nachrüstbare Methanolanlage für Verfahren von Essigsäure
EP2146166A2 (de) 1999-11-01 2010-01-20 Acetex (Cyprus) Limited Methanolanlagennachrüstung zur Herstellung von Essigsäure
EP2146166A3 (de) * 1999-11-01 2012-12-19 Acetex (Cyprus) Limited Methanolanlagennachrüstung zur Herstellung von Essigsäure
US6531630B2 (en) 2000-12-29 2003-03-11 Kenneth Ebenes Vidalin Bimodal acetic acid manufacture
WO2014143840A3 (en) * 2013-03-15 2014-12-04 Celanese International Corporation Process for separating product gas using carbonylation processes

Also Published As

Publication number Publication date
UA53620C2 (uk) 2003-02-17
CN1160300C (zh) 2004-08-04
EP0845452B2 (de) 2011-09-14
RU2196128C2 (ru) 2003-01-10
ATE221868T1 (de) 2002-08-15
JP3983868B2 (ja) 2007-09-26
DE69714554T2 (de) 2003-05-15
JPH10279516A (ja) 1998-10-20
DE69714554D1 (de) 2002-09-12
DE69714554T3 (de) 2012-02-02
EP0845452B1 (de) 2002-08-07
DK136196A (da) 1998-05-30
CN1188099A (zh) 1998-07-22
US5840969A (en) 1998-11-24

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